JPS60218579A - Method and device for liquefying gas - Google Patents
Method and device for liquefying gasInfo
- Publication number
- JPS60218579A JPS60218579A JP60062186A JP6218685A JPS60218579A JP S60218579 A JPS60218579 A JP S60218579A JP 60062186 A JP60062186 A JP 60062186A JP 6218685 A JP6218685 A JP 6218685A JP S60218579 A JPS60218579 A JP S60218579A
- Authority
- JP
- Japan
- Prior art keywords
- pressure
- gas
- liquid
- heat exchanger
- cooling device
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims description 17
- 239000007788 liquid Substances 0.000 claims description 93
- 239000007789 gas Substances 0.000 claims description 68
- 238000001816 cooling Methods 0.000 claims description 44
- 238000009833 condensation Methods 0.000 claims description 13
- 230000005494 condensation Effects 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 11
- 239000002808 molecular sieve Substances 0.000 claims description 9
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 9
- 239000011555 saturated liquid Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims 2
- 239000002912 waste gas Substances 0.000 claims 1
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 116
- 229910052757 nitrogen Inorganic materials 0.000 description 42
- 229910001873 dinitrogen Inorganic materials 0.000 description 32
- 238000010586 diagram Methods 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000003570 air Substances 0.000 description 3
- 230000003287 optical effect Effects 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 229910001882 dioxygen Inorganic materials 0.000 description 2
- 239000011810 insulating material Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000282376 Panthera tigris Species 0.000 description 1
- 229920005830 Polyurethane Foam Polymers 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000110 cooling liquid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000011496 polyurethane foam Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
- F25J1/0276—Laboratory or other miniature devices
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0012—Primary atmospheric gases, e.g. air
- F25J1/0015—Nitrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0225—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using other external refrigeration means not provided before, e.g. heat driven absorption chillers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/908—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by regenerative chillers, i.e. oscillating or dynamic systems, e.g. Stirling refrigerator, thermoelectric ("Peltier") or magnetic refrigeration
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/42—Modularity, pre-fabrication of modules, assembling and erection, horizontal layout, i.e. plot plan, and vertical arrangement of parts of the cryogenic unit, e.g. of the cold box
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Clinical Laboratory Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
(57)【要約】本公報は電子出願前の出願データであるた
め要約のデータは記録されません。(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.
Description
【発明の詳細な説明】
本発明はガス供給装置によって供給した大気圧より大き
い第1圧力のガスを冷却装置に供給し、次いで生成液体
を前記第1圧力に等しいかこれより低い第2圧力にする
ことにより前記ガスを液化する方法に関するものである
。さらに本発明は1j;1記方法を実施するための液化
装置に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention provides gas at a first pressure greater than atmospheric pressure supplied by a gas supply device to a cooling device, and then brings the produced liquid to a second pressure equal to or lower than said first pressure. The present invention relates to a method of liquefying the gas by doing so. Furthermore, the present invention relates to a liquefaction apparatus for implementing the method 1j;1.
冒頭に記載した種類の既知方法(1979年米国ハウス
トンで開催されたG A S T E C11会議にお
いて提供された[圧力揺動吸着によるLNG /Lr’
G船用窒素(Nitrogen for LNG /L
PG 5hips by pressureswing
adsorption)Jという標題のニー、エム。Known methods of the type mentioned at the outset (presented at the GASTE C11 conference held in Houston, USA in 1979 [LNG/Lr' by pressure swing adsorption]
Nitrogen for LNG /L
PG 5hips by pressure swing
adsorption) J.
フエイブシュ等の刊行物に開示されている)では、冷却
装置で凝縮させた窒素ガスを液態で貯蔵容器中に捕集し
ている。寒冷の漏洩によってこの貯蔵容器内で蒸発する
窒素を冷却装置に戻し、ここで再度凝縮させて貯蔵容器
内の液体窒素のレベルを維持している。ガス分離装置が
役に立たない場合には、液体窒素は貯蔵容器から蒸発器
に供給され次いでガス状態で使用者に供給される。勿論
のことではあるか、液体窒素を貯蔵容器から直接取出す
こともできが、既知装置は第一にこれを目的として設計
されていない。(as disclosed in the publication by Feibusch et al.), nitrogen gas is condensed in a cooling device and collected in liquid form in a storage vessel. Nitrogen that evaporates within the storage vessel due to refrigeration leakage is returned to the cooling system where it is recondensed to maintain the level of liquid nitrogen within the storage vessel. If a gas separation device is not available, liquid nitrogen is fed from a storage container to an evaporator and then delivered in gaseous form to the user. Of course, it is also possible to remove liquid nitrogen directly from the storage container, but known devices are not primarily designed for this purpose.
既知方法の欠点は、液体窒素を貯蔵容器から取出した後
に、貯蔵容器と使用者との間の通路に沿った寒冷の漏洩
および/または圧力低下によって窒素ガスが生成するこ
とで、使用者が液体窒素を望む場合には窒素ガスは使用
者にとってほとんど価値がない。しかも生成する窒素ガ
スはある分量の寒冷が利用されていないことを示す。さ
らに、冷却装置の位置は冷却装置が既に凝縮している戻
り液で一杯になるのを防止するために貯蔵容器の頂部に
限定される。A disadvantage of the known method is that, after the liquid nitrogen has been removed from the storage container, nitrogen gas is generated due to cold leakage and/or pressure drop along the path between the storage container and the user, and the user cannot remove the liquid from the storage container. Nitrogen gas is of little value to the user if nitrogen is desired. Moreover, the nitrogen gas produced indicates that a certain amount of refrigeration is not being utilized. Furthermore, the location of the cooling device is limited to the top of the storage vessel to prevent the cooling device from filling up with already condensed return liquid.
本発明の目的は前記欠点を有していない冒頭に記載した
方法を提供することにある。The object of the invention is to provide a method as described at the outset, which does not have the above-mentioned disadvantages.
また本発明の目的は本発明方法を実施するための液化装
置を提供することにある。Another object of the present invention is to provide a liquefaction device for carrying out the method of the present invention.
本発明方法は、前記ガス供給装置から流出する前記ガス
を第1ガス/ガス熱交換器に通して冷却した後に前記冷
却装置に供給し、しかる後に前記冷却装置内で凝縮によ
り生成する飽和液体および湿り蒸気を液体分離器に導き
、前記液体分離器から放出される前記飽和液体および前
記液体分離器の後で膨張により生成する前記湿り蒸気を
熱絶縁貯槽内に既に生成している液体中に位置する第2
熱交換器に導き、前記飽和液体および前記湿り蒸気をこ
の第2熱交換器においてそれぞれザブクーリングおよび
凝縮・サブクーリングし、サブクーリング程度を前記第
2熱交換器に連結されている圧力制御器によって達成し
、しかる後に前記第2圧力を前記冷却装置内の圧力に等
しい前記第2圧力の最大値に相当する値と前記貯槽内の
圧力に等しい前記第2圧力の最小値に相当する値との間
に調節し、かつ凝縮熱およびサブクーリング熱を利用し
て前記熱絶縁貯槽内に存在する液体の一部を蒸発させ、
これにより生成する蒸気を前記第1熱交換器に導いて前
記ガス供給装置により供給される前記ガスを冷却し、前
記貯槽内で蒸発した液体を前記液体分離器の下流に連結
されている供給導管によって補給することを特徴とする
。The method according to the invention comprises supplying the gas flowing out of the gas supply device to the cooling device after cooling it through a first gas/gas heat exchanger, and subsequently producing a saturated liquid and a liquid by condensation in the cooling device. directing the wet vapor to a liquid separator, placing the saturated liquid discharged from the liquid separator and the wet vapor produced by expansion after the liquid separator into the liquid already forming in a thermally insulated storage tank; Second to do
The saturated liquid and the wet vapor are subcooled and condensed/subcooled in the second heat exchanger, respectively, and the degree of subcooling is controlled by a pressure controller connected to the second heat exchanger. achieving and then adjusting said second pressure between a value corresponding to a maximum value of said second pressure equal to the pressure in said cooling device and a value corresponding to a minimum value of said second pressure equal to the pressure in said reservoir. and evaporate a portion of the liquid present in the thermally insulated storage tank using condensation heat and subcooling heat;
The vapor thus generated is guided to the first heat exchanger to cool the gas supplied by the gas supply device, and the liquid evaporated in the storage tank is transferred to a supply conduit connected downstream of the liquid separator. It is characterized by being replenished by.
本発明の液化装置は、ガス供給装置によって供給される
大気圧より大きい第1圧力のガスを冷却装置に供給し、
次いで生成液体を前記第1圧力に等しいかこれより低い
第2圧力にすることにより前記ガスを液化するガス液化
装置において、前記ガス供給装置の出I」は熱絶縁され
た第1熱交換器に連結され、前記第1熱交換器は第2熱
交換器および液体分離器と共に熱絶縁貯槽内に位置しか
つ冷却装置に連結され、前記冷却装置は前記熱絶縁貯槽
の外側に配置されていて、前記冷却装置の液体導管は前
記液体分離器に連結され、前記液体分離器は出口導管を
有し、前記出口導管は前記第2熱交換器に連結されかつ
圧力制御器を経て使用者に連結されており、前記圧力制
御器の開き圧力は使用者圧力とは無関係であり、さらに
前記熱絶縁容器にはレベル制御f11器が設けられてお
り、前記レベル制御器は前記液体分離器の出口導管に連
結されていることを特徴とする。The liquefaction device of the present invention supplies gas at a first pressure higher than atmospheric pressure supplied by the gas supply device to the cooling device,
In a gas liquefaction device that then liquefies the gas by bringing the produced liquid to a second pressure equal to or lower than the first pressure, the output I of the gas supply device is connected to a thermally insulated first heat exchanger. coupled, the first heat exchanger, together with a second heat exchanger and a liquid separator, being located within a thermally insulated reservoir and coupled to a cooling device, the cooling device being located outside of the thermally insulating reservoir; A liquid conduit of the cooling device is connected to the liquid separator, the liquid separator having an outlet conduit, the outlet conduit being connected to the second heat exchanger and to a user via a pressure controller. the opening pressure of the pressure controller is independent of the user pressure; and the thermally insulated vessel is provided with a level control f11, the level controller being connected to the outlet conduit of the liquid separator. It is characterized by being connected.
寒冷の漏洩および/または圧力低下に起因する蒸発を回
避するために多少強くサブクーリングした低温液体(c
ryogenic 1iquid)を供給装置から使用
者に輸送すること自体は米国特許第4,296,610
明細書から既知である。しかし、凝縮およびザブクーリ
ング中に放出される凝縮熱およびサブクーリング熱が失
なわれ、冷却用液体の温度」二51および圧力上昇を招
くことさえあり、かかる欠点を消滅する必要かある。The cryogenic liquid (c
ryogenic 1equid) from a supply device to a user is itself described in U.S. Pat. No. 4,296,610.
Known from the specification. However, the heat of condensation and subcooling released during condensation and subcooling is lost, which can even lead to an increase in the temperature and pressure of the cooling liquid, and there is a need to eliminate such drawbacks.
次に本発明を図面を参照して例について説明する。The invention will now be explained by way of example with reference to the drawings.
第1図に示す液化装置はガス分離装置12の形態のガス
供給装置を具え、このガス分離装置は2個の分子ふるい
14および16を具える。ガス分離装置12ばそれ自体
既知の種類のもので、例えばX4.F+41燃料(Fu
el) j第60巻、第817−822頁(1981年
9月号)に記載されているような装置である。人口導管
18を経て圧縮機20により空気を吸込め、この空気を
例えば6.5 kP (キロパスカル)で出に1導管2
2中に送り出す。出口導管22はコック24および26
によりそれぞれ分子ふるい14および16に連結するこ
とができる。分子ふるい14および16はさらにコック
28,30および32により出口導管34に連結されて
おり、この導管に真空ポンプ36を配置することができ
る。圧縮機20が比較的高い例えば6.5kPの送出し
圧力を有している場合には、真空ポンプ36をはふくこ
とができる。分子ふるい14および16は酸素ガスから
窒素ガスを分離する。酸素ガスはこれらのふるい内に残
留し、窒素ガスはコ・ツク38゜40および42を経て
供給導管44中に送り出される。The liquefier shown in FIG. 1 comprises a gas supply in the form of a gas separator 12 which comprises two molecular sieves 14 and 16. The liquefier shown in FIG. The gas separation device 12 is of a type known per se, for example X4. F+41 fuel (Fu
el) J, Vol. 60, pp. 817-822 (September 1981 issue). Air is sucked in by a compressor 20 through an artificial conduit 18, and this air is outputted through a conduit 2 at a pressure of, for example, 6.5 kP (kilopascal).
Send it out during 2nd. Outlet conduit 22 is connected to cocks 24 and 26
can be linked to molecular sieves 14 and 16, respectively. The molecular sieves 14 and 16 are further connected by cocks 28, 30 and 32 to an outlet conduit 34 in which a vacuum pump 36 can be arranged. If the compressor 20 has a relatively high delivery pressure, for example 6.5 kP, the vacuum pump 36 can be turned off. Molecular sieves 14 and 16 separate nitrogen gas from oxygen gas. Oxygen gas remains within these sieves and nitrogen gas is pumped into supply conduit 44 via ports 38, 40 and 42.
コック24,26,28,30,32,38.40およ
び42を交互に開閉する場合には、常にふるい14およ
び1Gの一方は窒素ガスを供給導管44中に送り出すの
に使用され、かつ他方のふるいは吸収酸素を大気に吹き
飛ばずことにより清浄になる。そこで平均圧力6.5
kPの窒素ガス流が得られる。窒素ガスは供給導管44
を経て熱絶縁貯槽48中、特にこの貯槽内に配置されて
いるガス/ガス熱交換、器50中に送り出される。窒素
ガスは熱交換器50に1において入り、熱交換器50を
2において離れる。符号I〜IOは本発明方法の熱力学
的手順を第4図および第5図に関して説明する゛ために
も使用されており、第4図および第5図には対応する符
号1〜10がイ」いている。1における窒素ガスハフ、
度は288 °にである。熱交換器50では、288
°にの窒素ガスは78°にの冷窒素ガスにより243″
Kに予備冷却され、この冷窒素ガスは熱交換器50に9
において入り、この熱交換器を10において離れる。そ
の時この冷窒素ガスは288 °Kに加熱されている。If the cocks 24, 26, 28, 30, 32, 38. The sieves are cleaner by not blowing the absorbed oxygen out into the atmosphere. So the average pressure is 6.5
A nitrogen gas flow of kP is obtained. Nitrogen gas is supplied through the supply conduit 44
via a thermally insulated storage tank 48 and, in particular, into a gas/gas heat exchanger 50 arranged within this storage tank. Nitrogen gas enters heat exchanger 50 at 1 and leaves heat exchanger 50 at 2. Reference numbers I to IO are also used to explain the thermodynamic procedure of the method according to the invention with respect to FIGS. 4 and 5, where corresponding reference numbers 1 to 10 are used. "I'm here." Nitrogen gas huff in 1,
The degree is 288°. In the heat exchanger 50, 288
Nitrogen gas at 78° is 243″ by cold nitrogen gas at 78°
This cold nitrogen gas is pre-cooled to a temperature of
It enters the heat exchanger at 10 and leaves the heat exchanger at 10. This cold nitrogen gas is then heated to 288°K.
熱交換器50において寒冷を伝達するために2個の同心
パイプを使用し、比較的高い温度の窒素ガスを内側パイ
プ内にかつ比較的低い温度の窒素ガスを外側パイプと内
側パイプとの間に通すことができる。熱交換器50は貯
槽48の内部から、例えば、ポリウレタンフォームのよ
うな絶縁材料51(液体2)により熱的に絶縁されてい
る。熱交換器50用冷窒素ガスを得る方法についてさら
に説明する。Two concentric pipes are used to transfer cold in the heat exchanger 50, with relatively high temperature nitrogen gas in the inner pipe and relatively low temperature nitrogen gas between the outer and inner pipes. Can pass. The heat exchanger 50 is thermally insulated from the interior of the reservoir 48 by an insulating material 51 (liquid 2), for example polyurethane foam. A method for obtaining cold nitrogen gas for the heat exchanger 50 will be further explained.
予備冷却された窒素ガスは熱交換器50を243 °に
の温度で離れ、導管52を経て冷却装置54に導かれる
。冷却装置54はそれ自体既知の種類のもので、例えば
ジエイ、ダブリュ、エル、ケラ−およびシー、オー、ジ
ョンカースが「フィリップス・テクニカル・レビュー」
、第16巻、第105〜115頁(1954年10月号
)に記載しているような装置である。この冷却装置は熱
交換器56を収容しており、この熱交換器56により3
において温度243 °におよび圧力6.5 kPで入
る窒素ガスが凝縮する。液体窒素は熱交換器56を4に
おいて温度96°におよび圧力6.5 kPで離れる。The precooled nitrogen gas leaves heat exchanger 50 at a temperature of 243° and is conducted via conduit 52 to cooling device 54 . The cooling device 54 is of a type known per se, for example by J.H., W., L., Keller and C.H., O., Jonkers, "Philips Technical Review".
, Vol. 16, pp. 105-115 (October 1954 issue). This cooling device houses a heat exchanger 56, which allows three
The nitrogen gas entering at a temperature of 243° and a pressure of 6.5 kP condenses. The liquid nitrogen leaves the heat exchanger 56 at 4 at a temperature of 96° and a pressure of 6.5 kP.
冷却装置54は導管58により熱絶縁貯槽48内に配置
されている液体トラ・ノブ60の形態の液体分離器に連
結されている(第3図も参照のこと)。液体窒素62は
液体トラップ60の下部で捕集される。この液体窒素の
上にはガス状窒素64が存在しており、このガス状窒素
は冷却装置54からのもので、このガス状窒素64を液
化装置の始動段階中に圧力つりあい導管65(破線)を
経て1952中に吹き出させて導管58内の液体窒素が
冷却装置54に戻らないようにする。液体窒素のレベル
66が所定の高さに到達すると直ちに、弁68かフロー
ト67によって開き、液体窒素が導管70中に送り出さ
れる。導管70は液体トラップ60を貯槽48内に配置
されている液/液ガス熱交換器72(第2熱交換器)に
連結する。熱交換器72は液化プロセスの始動段階中に
生成する78°にの液体窒素74中に位置する。熱交換
器72では、5において熱交換器に入る温度91°にの
液体窒素は7における温度78°Kまでそれぞれ冷却お
よびサブクーリングされる。さらに、液体トラップ60
による圧力低下によって生成する窒素ガスは符号5−6
によって示される経路に沿って再度凝縮し、次いで符号
6−7によって示される経路に沿ってサブクーリングさ
れる。熱交換器72の下流にはT分岐76が配置されて
いる。このT分岐において導管78は熱交換器72を圧
力制御器80に連結し、供給導管82ば熱交換器72を
レベル制御器84に連結する。レベル制御器84につい
てはさらに説明する。The cooling device 54 is connected by a conduit 58 to a liquid separator in the form of a liquid tiger knob 60 located within the thermally insulated reservoir 48 (see also FIG. 3). Liquid nitrogen 62 is collected at the bottom of liquid trap 60. Above this liquid nitrogen is gaseous nitrogen 64, which comes from the refrigeration system 54 and which is transferred to a pressure balance conduit 65 (dashed line) during the start-up phase of the liquefier. 1952 to prevent liquid nitrogen in conduit 58 from returning to cooling device 54. As soon as the liquid nitrogen level 66 reaches a predetermined height, either the valve 68 or the float 67 opens and liquid nitrogen is pumped into the conduit 70. Conduit 70 connects liquid trap 60 to a liquid/liquid gas heat exchanger 72 (second heat exchanger) located within reservoir 48 . Heat exchanger 72 is located in liquid nitrogen 74 at 78°, which is generated during the start-up phase of the liquefaction process. In the heat exchanger 72, the liquid nitrogen at a temperature of 91° entering the heat exchanger at 5 is cooled and subcooled to a temperature of 78°K at 7, respectively. Furthermore, the liquid trap 60
The nitrogen gas generated by the pressure drop due to
and then subcooled along the path indicated by 6-7. A T-branch 76 is arranged downstream of the heat exchanger 72. At this T-junction, conduit 78 connects heat exchanger 72 to pressure controller 80 and supply conduit 82 connects heat exchanger 72 to level controller 84 . The level controller 84 will be further explained.
第3図では詳細に示しかつ第2図では節ii′Lのため
に線図のみで示した圧力制御器80は貯槽48内に配置
されている。圧力制御器80は弁を具え、この弁は円板
弁素子88を具え、弁素子88はロッド90により円板
形支持体92に固定されている。円板弁素子88の表面
および液体窒素が上を流れる円板形支持体92の表面は
面積を等しくするのが好ましい。A pressure regulator 80, shown in detail in FIG. 3 and only diagrammatically for node ii'L in FIG. 2, is arranged in the reservoir 48. The pressure regulator 80 comprises a valve comprising a disc valve element 88 which is secured by a rod 90 to a disc-shaped support 92 . Preferably, the surface of the disc valve element 88 and the surface of the disc-shaped support 92 over which liquid nitrogen flows are equal in area.
開き圧力より小さい場合には、弁素子88は導管78内
に固定されている環状弁座94に掛合している。Below the opening pressure, the valve element 88 engages an annular valve seat 94 which is secured within the conduit 78 .
比較的ゆるい波形のベロー96が一端で支持体92にま
た他端でスリーブ98に固定され、スリーブ98は導管
78内に固定されている。スリーブ98には調整ねじ1
00を調整するためのねし山が設けられている。調整ね
じ100と支持体92との間にコイルばね102が配置
されている。コイルばね102はペロー96より硬い。A relatively loosely corrugated bellows 96 is secured at one end to the support 92 and at the other end to a sleeve 98, which is secured within the conduit 78. The sleeve 98 has an adjustment screw 1.
A screw thread is provided for adjusting 00. A coil spring 102 is arranged between the adjustment screw 100 and the support body 92. Coil spring 102 is harder than Perot 96.
弁素子88が開いている場合には導管78は弁座94中
の通路104によって導管106と連通ずる。導管10
6は貯蔵容器108に連結され、貯蔵容器108は出口
導管110を有し、導管110には使用者のためのコッ
ク112が設けられでいる。ばね102のプレストレス
がVに等しくかつ支持体92および弁素子88の表面積
が八に等しい場合には、開き圧力p+はV/Aに等しい
。このことば開き圧力1]+が導管106および貯蔵容
器10B内の使用者圧力p2(第2圧力)とは無関係で
あることを意味する。When valve element 88 is open, conduit 78 communicates with conduit 106 by passage 104 in valve seat 94. Conduit 10
6 is connected to a storage container 108, which has an outlet conduit 110, which is provided with a stopcock 112 for the user. If the prestress of spring 102 is equal to V and the surface areas of support 92 and valve element 88 are equal to 8, the opening pressure p+ is equal to V/A. This term means that the opening pressure 1]+ is independent of the user pressure p2 (second pressure) in the conduit 106 and the storage vessel 10B.
従って、プレストレス■を調整することにより、液体ト
ラップによる圧力低下を調整することができる。Therefore, by adjusting the prestress (2), the pressure drop due to the liquid trap can be adjusted.
レベル制御器84は弁114(第2図参照)を有し、フ
ロー目16により弁114を開閉することができ、フロ
ート116は貯槽48内の液体窒素のレベル11Bに従
って上下動する。弁114が開くと、液体窒素が導管1
20を経て貯槽48内の液体窒素74に添加される。液
化装置の始動段階では、冷却装置54はレベル118が
弁114を閉じた場合の高さに到達するまで液体窒素を
貯槽48に供給する。熱交換器72内の液体窒素および
ガス状窒素は絶えず熱を液体窒素74に与えるので、液
体窒素74の一部分は連続的に蒸発する。この蒸発した
78°にの窒素は9においてガス/ガス熱交換器50に
供給され、ガス分離装置12によって供給した窒素ガス
を予(1ifi冷却するのに用いられる。熱交換器72
によって蒸発した貯槽48内の窒素は絶えずレベル制御
器84によって補給される。またレベル制御器84は液
体トラップ60の下流で導管70に連結することができ
る。The level controller 84 has a valve 114 (see FIG. 2), which can be opened and closed by a flow eye 16, and the float 116 moves up and down according to the level 11B of liquid nitrogen in the reservoir 48. When valve 114 opens, liquid nitrogen enters conduit 1.
20 and added to the liquid nitrogen 74 in the storage tank 48. During the start-up phase of the liquefier, the cooling device 54 supplies liquid nitrogen to the reservoir 48 until the level 118 reaches the height it would have if the valve 114 were closed. Since the liquid nitrogen and gaseous nitrogen in heat exchanger 72 continually impart heat to liquid nitrogen 74, a portion of liquid nitrogen 74 is continuously vaporized. This evaporated nitrogen at 78° is fed to the gas/gas heat exchanger 50 at 9 and is used to pre-cool the nitrogen gas fed by the gas separation device 12. Heat exchanger 72
The nitrogen in the storage tank 48 that has been evaporated is constantly replenished by the level controller 84. A level controller 84 can also be coupled to conduit 70 downstream of liquid trap 60.
本発明方法およびその可能性を第4図および第5図につ
いて一層詳細に説明する。第4図および第5図において
逐次符号1〜10によって示されるような方法において
プレストレス■を増大した場合には、開き圧力p+は、
例えば、符号5’、6′および7′によって示されるレ
ベルまで上昇する。The method of the invention and its possibilities will be explained in more detail with reference to FIGS. 4 and 5. If the prestress ■ is increased in the manner indicated by the sequential numbers 1 to 10 in FIGS. 4 and 5, the opening pressure p+ is
For example, it rises to the levels indicated by 5', 6' and 7'.
サブクーリング程度は経路6−7と経路5’−7’との
間の長さの差によって決まる量たけ増大する。The degree of subcooling increases by an amount determined by the length difference between paths 6-7 and 5'-7'.
そこでサブクーリングエンタルピーΔ110 と凝1宿
エンタルピーΔ11c との比は変化するが、サブクー
リングエンタルピーと凝縮エンタルピーとの和ΔH−Δ
H,+Δしは一定のままである。従って、熱交換器72
内の液体窒素およびガス状窒素によつ−て貯槽48内の
液体窒素74に与えられる全熱量(経路8−9)は常に
等しい値であり、熱交換器50の冷却能力に丁度等しい
。使用者圧力p2はp。とpmaxとの間の値であるこ
とができるので、Δいの量だけ変動することができる。Therefore, the ratio between subcooling enthalpy Δ110 and condensation enthalpy Δ11c changes, but the sum of subcooling enthalpy and condensation enthalpy ΔH−Δ
H and +Δ remain constant. Therefore, the heat exchanger 72
The total amount of heat imparted to liquid nitrogen 74 in reservoir 48 (paths 8-9) by the liquid nitrogen and gaseous nitrogen in storage tank 48 is always equal and exactly equal to the cooling capacity of heat exchanger 50. The user pressure p2 is p. and pmax, so it can vary by an amount of Δ.
従って、サービス圧力p2が増減するにつれて、取出し
液体窒素のサブクーリング程度が増減する。Therefore, as the service pressure p2 increases or decreases, the degree of subcooling of the extracted liquid nitrogen increases or decreases.
第2圧力すなわち使用者圧力p2が開き圧力p1より低
くかつ貯槽内の圧力p0より大きいかあるいはこれに等
しい(ずなわちp。≦pz<T1+である)場合には、
使用者によって達成される。サブクーリングは熱交換器
72によって達成されるサブクーリングΔI+、より小
さい。液体トラップ60と圧力制御器80との間の圧力
はこの場合には一定不変でplであり、この理由は圧力
制御器80がplより高い圧力で閉止されるからである
。使用者圧力p2がpmaxより小さいかあるいはこれ
に等しくかつ開き圧力p、より大きい(すなわちI)I
<I)2≦p188である)場合には、使用者によって
達成されるサブクーリングは第2熱交換器72によって
達成されるサブクーリングΔH,より大きい。液体トラ
ップ60と圧力制御器80との間の圧力は今度はp2に
なる。If the second pressure or user pressure p2 is lower than the opening pressure p1 and greater than or equal to the pressure in the reservoir p0 (ie p.≦pz<T1+), then
achieved by the user. The subcooling is less than the subcooling ΔI+ achieved by heat exchanger 72. The pressure between the liquid trap 60 and the pressure regulator 80 is in this case constant pl, since the pressure regulator 80 is closed at a pressure higher than pl. The user pressure p2 is less than or equal to pmax and the opening pressure p is greater (i.e. I) I
<I)2≦p188), the subcooling achieved by the user is greater than the subcooling ΔH, achieved by the second heat exchanger 72. The pressure between liquid trap 60 and pressure controller 80 is now p2.
使用者圧力p2が開き圧力p1に等しい場合には、使用
者によって達成されるザブクーリングは熱交換器72に
よって達成されるサブクーリングΔHoに等しい。液体
トラップ60と圧力制御器80との間の圧力は今度はp
+=pzである。このよ・うにして、使用者がサブクー
リング程度および使用者圧力を所望のように変えること
ができるという成果が得られる。コック112により、
使用者は液体窒素を取出すことができる。使用者圧力p
2は、減圧コック113および蒸発器115を設け、導
管117を経て貯蔵容器108にフィードハックし、周
囲温度にすることにより、調整することができる。この
ことは極めて重要であって、その理由は常に使用者側で
起る圧力損失がもはや窒素ガスの生成をもたらさないか
らである。この圧力損失に適合させることのできる使用
者にとってのサブクーリング程度は事実使用者圧力p2
と貯槽48内の圧力p。If the user pressure p2 is equal to the opening pressure p1, the subcooling achieved by the user is equal to the subcooling ΔHo achieved by the heat exchanger 72. The pressure between liquid trap 60 and pressure controller 80 is now p
+=pz. In this way, the result is that the user can vary the degree of subcooling and the user pressure as desired. By cook 112,
The user can extract liquid nitrogen. User pressure p
2 can be regulated by providing a vacuum cock 113 and an evaporator 115 with a feed hack to the storage vessel 108 via conduit 117 to bring it to ambient temperature. This is extremely important, since the pressure loss that always occurs on the user side no longer results in the formation of nitrogen gas. The degree of subcooling for the user that can be adapted to this pressure loss is in fact the user pressure p2
and the pressure p in the storage tank 48.
との圧力差(第4図参照)によって決まる。使用者にと
ってサブクーリングされた液体窒素が必要である場合に
は、使用者圧力p2は貯槽48内の圧力poより高くな
るので圧力p。(符号8)にはならない。貯槽48内の
圧力p。は大気圧に等しいことが多い。圧力制御器80
によって、液体トラップ60による圧力低下、従って第
4図の経路5−7のレベルが決まるので、圧力制御器の
調節によって熱交換器72における熱交換のための経路
5−7に沿った利用可能な温度差も決まる(第5図参照
)。(see Figure 4). If the user requires subcooled liquid nitrogen, the user pressure p2 will be higher than the pressure po in the storage tank 48, so the pressure p. (Symbol 8) is not achieved. Pressure p in reservoir 48. is often equal to atmospheric pressure. pressure controller 80
determines the pressure drop across liquid trap 60 and thus the level of path 5-7 in FIG. The temperature difference is also determined (see Figure 5).
第2図に示す貯槽48の例では、熱交換器50は2本の
同心パイプ(図面では見えない)からなる。In the example of storage tank 48 shown in FIG. 2, heat exchanger 50 consists of two concentric pipes (not visible in the drawing).
ガス分離装置12の窒素ガスは導管44を経て1におい
て熱交換器50に入り、導管52(第2図では導管58
の後方に位置する)を経て2において熱交換器を離れ、
導管52は冷却装置54に連結されている。Nitrogen gas from the gas separator 12 enters the heat exchanger 50 at 1 via conduit 44 and passes through conduit 52 (in FIG. 2 conduit 58).
2) leaves the heat exchanger at 2,
Conduit 52 is connected to cooling device 54 .
貯槽48内で蒸発した冷窒素ガスは熱交換器50に9に
おいて入り、この熱交換器を10において離れる。The cold nitrogen gas evaporated in reservoir 48 enters heat exchanger 50 at 9 and leaves this heat exchanger at 10.
熱交換器は向流原理に従って行われる。熱交換器50に
おいて加熱された窒素ガスは貯槽48から出て周囲空気
に導かれるので、貯槽48内では大気圧(0,98kP
)が優勢である。圧力制御器が周囲空気への導管に組込
まれている場合には、貯槽48内で大気圧より大きい圧
力を得ることができる。この場合には、第4図の圧力−
エンタルピー図において、経路8−9−10は一層高い
圧力レベルに位置する。従って、経路5−6−7に沿っ
た凝縮エンタルピーとサブクーリングエンタルピーとの
比(一定な凝縮エンタルピーにおける)のほか、2種の
エンタルピーの和、従って予備冷却に利用できる貯槽4
8から蒸発した窒素量が変化する。このようにして予備
冷却程度を調整することができる。The heat exchanger is carried out according to the countercurrent principle. The nitrogen gas heated in the heat exchanger 50 exits the storage tank 48 and is guided into the surrounding air, so that the atmospheric pressure (0.98 kP) is maintained within the storage tank 48.
) is predominant. If a pressure controller is integrated in the conduit to the ambient air, a pressure greater than atmospheric pressure can be obtained in the reservoir 48. In this case, the pressure in Figure 4 -
In the enthalpy diagram, paths 8-9-10 are located at higher pressure levels. Therefore, in addition to the ratio of condensation enthalpy and subcooling enthalpy along path 5-6-7 (at constant condensation enthalpy), the sum of the two enthalpies and therefore the storage tank 4 available for precooling
The amount of nitrogen evaporated from 8 changes. In this way, the degree of preliminary cooling can be adjusted.
窒素を使用した例について液化装置を説明したが、他の
物質、例えば酸素、水素、メタン、アルゴン等を使用す
ることでもできる。このためには、これらの物質に適合
したガス分離装置ff 12および冷却装置54を使用
することのみが必要である。ガス供給装置は分子ふるい
を具えるガス分離装置12に限定される訳ではない。ガ
スをその沸点差を利用して互に分離する既知のいわゆる
ガス分離カラムも使用である。かかる場合には、分離後
にガスを圧縮機により大気圧より大きい圧力にして冷却
装置を最適に利用できるようにする。冷却装置による寒
冷の生成は事実供給ガスの比較的高い圧力(比較的高い
凝縮温度)において増加するが、冷却装置の消費動力は
不変である。比較的高い凝縮温度では、冷却装置の例え
ばヘリウムガスのような作用媒体の圧力を上昇すること
ができるが、冷却装置の負荷は減少する。冷却装置に供
給される生成物ガスのために常圧より大きい圧力を使用
することにより、さらにポンプ装置を設ける必要はなく
なる。圧力は分子ふるいを具えるガス分離装置内に既に
存在している圧縮機により供給される。Although the liquefier has been described using nitrogen, other substances such as oxygen, hydrogen, methane, argon, etc. can also be used. For this purpose, it is only necessary to use a gas separation device ff 12 and a cooling device 54 that are compatible with these substances. The gas supply device is not limited to a gas separation device 12 comprising a molecular sieve. Known so-called gas separation columns, which separate gases from each other using their boiling point differences, can also be used. In such cases, after separation, the gas is brought to a pressure greater than atmospheric pressure by means of a compressor to allow optimal utilization of the cooling system. Although the production of refrigeration by the cooling device actually increases at higher pressures of the feed gas (relatively higher condensing temperatures), the power consumption of the cooling device remains unchanged. At relatively high condensation temperatures, the pressure of the working medium, such as helium gas, in the cooling system can be increased, but the load on the cooling system is reduced. By using a pressure greater than normal pressure for the product gas fed to the cooling device, there is no need for further pumping devices. The pressure is supplied by a compressor already present in the gas separation device comprising the molecular sieve.
あるいはまた導管44に供給するガスを貯蔵容器からの
ガスとすることができる。Alternatively, the gas supplied to conduit 44 can be from a storage container.
液体トラップ60の形態の液体分離器は二つの作用を行
う。第1に、冷却装置54からの飽和液体を冷却装置5
4からの湿り蒸気から分離する。さらに、液体トラップ
60は逆止め弁として作用するので、貯槽48が冷却装
置54より高いレベルに配置されている場合でも、液体
が冷却装置に逆流することはあり得ない。事実、液体ト
ラップの代りに、例えば、熱平衡状態にある飽和液体お
よび飽和蒸気を収容する容器のような、任意の液体分離
器を使用することができ、この場合にはフロートの代り
に光センサを使用する。光センサは液体分離器の弁を制
御する。またかかる光センサをレベル制御器におけるフ
ロートの代りに使用することができる。A liquid separator in the form of liquid trap 60 performs two functions. First, the saturated liquid from the cooling device 54 is transferred to the cooling device 5.
Separate from the wet steam from 4. Additionally, liquid trap 60 acts as a check valve so that even if reservoir 48 is located at a higher level than cooling device 54, liquid cannot flow back into the cooling device. In fact, instead of a liquid trap, any liquid separator can be used, for example a container containing a saturated liquid and a saturated vapor in thermal equilibrium, and in this case an optical sensor instead of a float can be used. use. The optical sensor controls the liquid separator valve. Such optical sensors can also be used in place of floats in level controllers.
本発明を288〜78°にの温度範囲温度および6.5
〜1kPの圧力範囲について説明したが、本発明はかか
る範囲に限定されるものではない。可能な作動範囲は当
該ガスの圧力−エンタルピー図および温度−エンタルピ
ー図によって与えるられる。The temperature range temperature from 288 to 78° and 6.5°
Although a pressure range of ~1 kP has been described, the present invention is not limited to this range. The possible operating range is given by the pressure-enthalpy and temperature-enthalpy diagrams of the gas in question.
第1図は本発明装置の一例の断面図、
第2図は第1図の装置における熱絶縁貯槽の拡大断面図
、
第3図は第2図の装置における圧力制御器の拡大断面図
、 1
第4図は本発明方法による圧力−エンタルピー図、 1
第5図は本発明方法による圧力−エントロピー図である
。
■・・・熱交換器50における窒素ガス入口2・・・熱
交換器50における窒素ガス出口3・・・熱交換器56
におりる窒素ガス入「14・・・熱交換器56における
液体窒素出口5・・・熱交換器72における液体窒素・
窒素ガス入口6・・・熱交換器72における窒素ガスの
凝縮終了点7・・・熱交換器72における液体窒素出口
9・・・熱交換器50における冷窒素ガス人口10・・
・熱交換器50における窒素ガス出口12・・・ガス分
離装置(ガス供給装置)14.16・・・分子ふるい
18・・・入口導管20・・・圧縮m 22・・・出口
導管24.26,28.30.32・・・コック34・
・・出口導管 36・・・真空ポンプ38.40.42
・・・コック 44・・・供給導管48・・・熱絶縁貯
槽
50・・・ガス/ガス熱交換器(第1熱交換器)51・
・・絶縁材料 52・・・導管
54・・・冷却装置 56・・・熱交換器58・・・導
管 60・・・液体トラップ(液体分離器)62・・・
液体窒素 64・・・ガス状窒素65・・・圧力つりあ
い導管
66・・・液体窒素レベル 67・・・フロート68・
・・弁 70・・・導管
72・・・液/?1にガス熱交換器(第2熱交換器)7
4・・・液体窒素 76・・・T分岐78・・・導管
80・・・圧力制御器82・・・供給導管 84・・・
レベル制御器88・・・弁素子 90・・・ロンド
92・・・支持体 94・・・弁座
96・・・ヘロー 98・・・スIJ −フ100・・
・ネj; 102・・・コイルばね104・・・通路
106・・・導管
108・・・貯蔵容器 112・・・コ・ツク113・
・・減圧コック 114・・・弁115・・・蒸発器
116・・・フロート117・・・導管 118・・・
液体窒素レベル120・・・導管
A・・・支持体82および弁素子88の表面積■・・・
ばね102のプレストレス
po・・・貯槽48内の圧力
pl・・・圧力制御器80におりる開き圧力p2・・・
使用者圧力(第2圧力、サービス圧力)Δ11.・・・
サブクーリングエンタルピー(熱交換器72によって達
成される)
ΔIIC・・・凝縮エンタルピー
ΔH・・・Δ10とΔl(わとの和1 is a sectional view of an example of the device of the present invention, FIG. 2 is an enlarged sectional view of a thermally insulated storage tank in the device of FIG. 1, and FIG. 3 is an enlarged sectional view of a pressure controller in the device of FIG. 2. FIG. 4 is a pressure-enthalpy diagram according to the method of the present invention, and FIG. 5 is a pressure-entropy diagram according to the method according to the present invention. ■...Nitrogen gas inlet 2 in heat exchanger 50...Nitrogen gas outlet 3 in heat exchanger 50...Heat exchanger 56
14...liquid nitrogen outlet 5 in the heat exchanger 56...liquid nitrogen gas in the heat exchanger 72
Nitrogen gas inlet 6...Nitrogen gas condensation end point 7 in heat exchanger 72...Liquid nitrogen outlet 9 in heat exchanger 72...Cold nitrogen gas population 10 in heat exchanger 50...
・Nitrogen gas outlet 12 in heat exchanger 50...Gas separation device (gas supply device) 14.16...Molecular sieve
18... Inlet conduit 20... Compression m 22... Outlet conduit 24.26, 28.30.32... Cock 34.
... Outlet conduit 36 ... Vacuum pump 38.40.42
... Cock 44 ... Supply conduit 48 ... Thermal insulation storage tank 50 ... Gas/gas heat exchanger (first heat exchanger) 51.
... Insulating material 52 ... Conduit 54 ... Cooling device 56 ... Heat exchanger 58 ... Conduit 60 ... Liquid trap (liquid separator) 62 ...
Liquid nitrogen 64... Gaseous nitrogen 65... Pressure balance conduit 66... Liquid nitrogen level 67... Float 68.
...Valve 70...Conduit 72...Liquid/? 1 gas heat exchanger (second heat exchanger) 7
4...Liquid nitrogen 76...T branch 78...Conduit
80... Pressure controller 82... Supply conduit 84...
Level controller 88...Valve element 90...Rondo 92...Support body 94...Valve seat 96...Hero 98...S IJ-F100...
・Nej; 102... Coil spring 104... Passage
106... Conduit 108... Storage container 112... Kotsuk 113...
...Reducing cock 114...Valve 115...Evaporator
116... Float 117... Conduit 118...
Liquid nitrogen level 120...Conduit A...Surface area of support 82 and valve element 88■...
Prestress po of the spring 102...Pressure pl in the storage tank 48...Opening pressure p2 going to the pressure controller 80...
User pressure (second pressure, service pressure) Δ11. ...
Subcooling enthalpy (achieved by heat exchanger 72) ΔIIC... Condensation enthalpy ΔH... Δ10 and Δl (sum of
Claims (1)
い第1圧力のガスを冷却装置に供給し、次いで生成液体
を前記第1圧力に等しいかこれより低い第2圧力にする
ことにより前記ガスを液化するに当り、 前記ガス供給装置から流出する前記ガスを第1ガス/ガ
ス熱交換器に通して冷却した後に前記冷却装置に供給し
、しかる後に前記冷却装置内で凝縮により生成する飽和
液体および湿り蒸気を液体分離器に導き、前記液体分離
器から放出される前記飽和液体および前記液体分離器の
後で膨張により生成する前記湿り蒸気を熱絶縁貯槽内に
既に生成している液体中に位置する第2熱交換器に導き
、前記飽 ′相液体および前記湿り蒸気をこの第2熱交
換器においてそれぞれサブクーリングおよび凝縮・サブ
クーリングし、サブクーリング程度を前記第2熱交換器
に連結されている圧力制御器に°よって達成し、しかる
後に前記第2圧力を前記冷却装置内の圧力に等しい前記
第2圧力の最大値に相当する値と前記貯槽内の圧力に等
しい前記第2圧力の最小値に相当する値との間に調節し
、かつ凝縮熱およびサブクーリング熱を利用して前記熱
絶縁貯槽内に存在する液体の一部を蒸発させ、これによ
り生成する蒸気を前記第1熱交換器に導いて前記ガス供
給装置により供給される前記カスを冷却し、前記貯槽内
で蒸発した液体を前記液体分離器の下流に連結されてい
る供給導管によって補給することを特徴とするガス液化
方法。 2、前記ガス供給装置が既知のガス分離装置であり、こ
の装置において大気圧のガス混合物の圧力を圧縮機によ
り大気圧より大きい第1圧力まで高め、次いで分子ふる
いに供給し、第1の種類のガス部分を通過させ、かつ第
2の種類のガス部分を吸収・脱離させ、しかる後に前記
第1の種類のガス部分を前記冷却装置に供給する特許請
求の範囲第1項記載の方法。 3、 ガス供給装置によって供給される大気圧より大き
い第1圧力のガスを冷却装置に供給し、次いで生成液体
を前記第1圧力に等しいかこれより低い第2圧力にする
ことにより前記ガスを液化するガス液化装置において、 前記ガス供給装置の出口は熱絶縁された第1熱交換器に
連結され、前記第1熱交換器は第2熱交換器および液体
分離器と共に熱絶縁貯槽内に位置しかつ冷却装置に連結
され、前記冷却装置は前記熱絶縁貯槽の外側に配置され
ていて、前記冷却装置の液体導管は前記液体分離器に連
結され、前記液体分離器は出口導管を有し、前記出口導
管は前記第2熱交換器に連結されかつ圧力制御器を経て
使用者に連結されており、前記圧力制御器の開き圧力は
使用者圧力とは無関係であり、さらに前記熱絶縁容器に
ばレベル制御器が設けられており、前記レベル制御器は
前記液体分離器の出口導管に連結されていることを特徴
とするガス液化装置。 4、 前記第2熱交換器も前記レベル制御器に連結され
ており、前記レベル制御器は弁を具え、前記弁は前記貯
槽内の液体の所定レベルにおいて開いて液体を前記第2
熱交換器から前記熱絶縁貯槽に供給することができる特
許請求の範囲第3項記載の装置。 5、 前記液体分離器が既知の液体トラップの形態であ
る特許請求の範囲第3項記載の装置。 6、 前記ガス供給装置が、このガス供給装置に供給さ
れるガス混合物から所望の種類のガスを分離するための
少くとも2個の分子ふるいを具える既知のガス分離装置
である特許請求の範囲第3項記載の装置。[Claims] 1. Supplying a gas at a first pressure greater than atmospheric pressure supplied by a gas supply device to a cooling device, and then subjecting the produced liquid to a second pressure equal to or lower than the first pressure. In order to liquefy the gas, the gas exiting the gas supply device is cooled by passing it through a first gas/gas heat exchanger before being supplied to the cooling device, and is then liquefied in the cooling device by condensation. The saturated liquid and moist vapor produced are led to a liquid separator, the saturated liquid discharged from the liquid separator and the moist vapor produced by expansion after the liquid separator already produced in a thermally insulated storage tank. The saturated liquid and the wet vapor are subcooled and condensed/subcooled in the second heat exchanger, respectively, and the subcooling level is transferred to the second heat exchanger. by means of a pressure controller connected to the cooling device, after which the second pressure is adjusted to a value corresponding to a maximum value of the second pressure equal to the pressure in the cooling device and a value equal to the pressure in the reservoir. a value corresponding to the minimum value of the second pressure, and evaporates a part of the liquid present in the thermally insulated storage tank using condensation heat and subcooling heat, thereby generating steam. The waste gas supplied by the gas supply device is guided to the first heat exchanger to cool it, and the liquid evaporated in the storage tank is replenished by a supply conduit connected downstream of the liquid separator. Gas liquefaction method. 2. The gas supply device is a known gas separation device, in which the pressure of the gas mixture at atmospheric pressure is increased by a compressor to a first pressure greater than atmospheric pressure, and then fed to a molecular sieve, 2. A method as claimed in claim 1, in which a gas fraction of a second type is passed through and a gas fraction of a second type is absorbed and desorbed, after which said gas fraction of a first type is supplied to said cooling device. 3. Liquefying the gas by supplying a gas at a first pressure greater than atmospheric pressure supplied by a gas supply device to a cooling device and then bringing the produced liquid to a second pressure equal to or lower than the first pressure. In the gas liquefaction apparatus, the outlet of the gas supply device is connected to a thermally insulated first heat exchanger, and the first heat exchanger is located in a thermally insulated storage tank together with a second heat exchanger and a liquid separator. and connected to a cooling device, the cooling device being disposed outside the thermally insulated storage tank, a liquid conduit of the cooling device being connected to the liquid separator, the liquid separator having an outlet conduit, and the liquid separator having an outlet conduit; An outlet conduit is connected to the second heat exchanger and to the user via a pressure controller, the opening pressure of the pressure controller being independent of the user pressure, and further connected to the thermally insulating container. Gas liquefaction device, characterized in that a level controller is provided, said level controller being connected to an outlet conduit of said liquid separator. 4. The second heat exchanger is also coupled to the level controller, the level controller comprising a valve that opens at a predetermined level of liquid in the reservoir to direct the liquid to the second heat exchanger.
4. The device of claim 3, wherein the thermally insulated reservoir can be supplied from a heat exchanger. 5. Apparatus according to claim 3, wherein the liquid separator is in the form of a known liquid trap. 6. The gas supply device is a known gas separation device comprising at least two molecular sieves for separating the desired type of gas from the gas mixture supplied to the gas supply device. The device according to paragraph 3.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
NL8400990A NL8400990A (en) | 1984-03-29 | 1984-03-29 | METHOD FOR LIQUEIFICATION OF A GAS AND LIQUEIFICATION PLANT FOR CARRYING OUT THE METHOD |
NL8400990 | 1984-03-29 |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS60218579A true JPS60218579A (en) | 1985-11-01 |
Family
ID=19843721
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP60062186A Pending JPS60218579A (en) | 1984-03-29 | 1985-03-28 | Method and device for liquefying gas |
Country Status (8)
Country | Link |
---|---|
US (1) | US4575386A (en) |
EP (1) | EP0158395B1 (en) |
JP (1) | JPS60218579A (en) |
BR (1) | BR8501364A (en) |
CA (1) | CA1242637A (en) |
DE (1) | DE3560690D1 (en) |
IN (1) | IN162167B (en) |
NL (1) | NL8400990A (en) |
Families Citing this family (16)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3524729A1 (en) * | 1985-07-11 | 1987-01-15 | Leybold Heraeus Gmbh & Co Kg | DEVICE FOR CLEANING SMOKE GASES SULFUR AND NITROGEN |
US4841732A (en) * | 1987-12-28 | 1989-06-27 | Sarcia Domenico S | System and apparatus for producing and storing liquid gases |
US4796433A (en) * | 1988-01-06 | 1989-01-10 | Helix Technology Corporation | Remote recondenser with intermediate temperature heat sink |
US4854128A (en) * | 1988-03-22 | 1989-08-08 | Zeamer Corporation | Cryogen supply system |
US5291738A (en) | 1992-12-07 | 1994-03-08 | Edwards Engineering Corp. | Vapor recovery apparatus and method |
US5415001A (en) * | 1994-03-25 | 1995-05-16 | Gas Research Institute | Liquefied natural gas transfer |
US5979440A (en) | 1997-06-16 | 1999-11-09 | Sequal Technologies, Inc. | Methods and apparatus to generate liquid ambulatory oxygen from an oxygen concentrator |
FR2769354B1 (en) * | 1997-10-06 | 1999-11-05 | Air Liquide | METHOD AND INSTALLATION FOR FILLING A PRESSURE TANK |
GB9813001D0 (en) * | 1998-06-16 | 1998-08-12 | Air Prod & Chem | Containment enclosure |
CR7129A (en) * | 2003-10-29 | 2003-11-17 | Carlos Eduardo Rold N Villalobos | METHOD AND APPARATUS FOR STORAGE GASES AT LOW TEMPERATURE USING A REFRIGERATION RECOVERY SYSTEM |
US7197884B2 (en) * | 2004-03-01 | 2007-04-03 | Christopher Jones | Assembly and method for cryo-preservation of specimens in a cryogen-free environment |
US7913497B2 (en) * | 2004-07-01 | 2011-03-29 | Respironics, Inc. | Desiccant cartridge |
US7318327B2 (en) * | 2004-10-26 | 2008-01-15 | Respironics In-X, Inc. | Liquefying and storing a gas |
DE102005028199A1 (en) * | 2005-06-17 | 2006-12-21 | Linde Ag | Storage container for kyrogenic media |
DE102011013577B4 (en) * | 2011-03-10 | 2013-02-28 | Karlsruher Institut für Technologie | Device for storing hydrogen and magnetic energy and a method for their operation |
US9821425B2 (en) | 2014-03-05 | 2017-11-21 | 5Me Ip, Llc | Device for supplying subcooled liquid cryogen to cutting tools |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
NL134862C (en) * | 1964-04-11 | |||
US3667246A (en) * | 1970-12-04 | 1972-06-06 | Atomic Energy Commission | Method and apparatus for precise temperature control |
FR2288956A1 (en) * | 1973-03-27 | 1976-05-21 | Commissariat Energie Atomique | PROCESS FOR REDUCING THE CONSUMPTION OF A CRYOSTAT AND CORRESPONDING DEVICE |
CH625609A5 (en) * | 1977-12-23 | 1981-09-30 | Sulzer Ag | |
US4277949A (en) * | 1979-06-22 | 1981-07-14 | Air Products And Chemicals, Inc. | Cryostat with serviceable refrigerator |
US4296610A (en) * | 1980-04-17 | 1981-10-27 | Union Carbide Corporation | Liquid cryogen delivery system |
JPS5880474A (en) * | 1981-11-06 | 1983-05-14 | 株式会社日立製作所 | Cryogenic cooling device |
-
1984
- 1984-03-29 NL NL8400990A patent/NL8400990A/en not_active Application Discontinuation
- 1984-09-17 US US06/651,485 patent/US4575386A/en not_active Expired - Fee Related
-
1985
- 1985-03-13 IN IN187/CAL/85A patent/IN162167B/en unknown
- 1985-03-25 DE DE8585200447T patent/DE3560690D1/en not_active Expired
- 1985-03-25 EP EP85200447A patent/EP0158395B1/en not_active Expired
- 1985-03-26 BR BR8501364A patent/BR8501364A/en unknown
- 1985-03-28 CA CA000477844A patent/CA1242637A/en not_active Expired
- 1985-03-28 JP JP60062186A patent/JPS60218579A/en active Pending
Also Published As
Publication number | Publication date |
---|---|
NL8400990A (en) | 1985-10-16 |
IN162167B (en) | 1988-04-09 |
EP0158395A1 (en) | 1985-10-16 |
DE3560690D1 (en) | 1987-10-29 |
CA1242637A (en) | 1988-10-04 |
US4575386A (en) | 1986-03-11 |
EP0158395B1 (en) | 1987-09-23 |
BR8501364A (en) | 1985-11-19 |
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